JPS62244378A - Device for pretreatment of filtration membrane - Google Patents
Device for pretreatment of filtration membraneInfo
- Publication number
- JPS62244378A JPS62244378A JP8981886A JP8981886A JPS62244378A JP S62244378 A JPS62244378 A JP S62244378A JP 8981886 A JP8981886 A JP 8981886A JP 8981886 A JP8981886 A JP 8981886A JP S62244378 A JPS62244378 A JP S62244378A
- Authority
- JP
- Japan
- Prior art keywords
- membrane
- fermentation
- gas
- tank
- membrane unit
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- 239000012528 membrane Substances 0.000 title claims abstract description 73
- 238000001914 filtration Methods 0.000 title abstract description 3
- 239000007788 liquid Substances 0.000 claims abstract description 16
- 244000005700 microbiome Species 0.000 claims abstract description 16
- 239000007789 gas Substances 0.000 claims description 25
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 claims description 6
- 229910001882 dioxygen Inorganic materials 0.000 claims description 6
- 230000002378 acidificating effect Effects 0.000 claims 1
- 238000003825 pressing Methods 0.000 claims 1
- 238000000855 fermentation Methods 0.000 abstract description 26
- 230000004151 fermentation Effects 0.000 abstract description 24
- 239000000203 mixture Substances 0.000 abstract description 5
- 230000010287 polarization Effects 0.000 abstract description 5
- 238000011109 contamination Methods 0.000 abstract description 2
- 239000000706 filtrate Substances 0.000 abstract 2
- 239000000758 substrate Substances 0.000 abstract 1
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 8
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 8
- 238000010586 diagram Methods 0.000 description 6
- 230000001580 bacterial effect Effects 0.000 description 5
- 238000005273 aeration Methods 0.000 description 4
- 238000006243 chemical reaction Methods 0.000 description 4
- 239000000126 substance Substances 0.000 description 3
- 238000000108 ultra-filtration Methods 0.000 description 3
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 2
- 235000014113 dietary fatty acids Nutrition 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 229930195729 fatty acid Natural products 0.000 description 2
- 239000000194 fatty acid Substances 0.000 description 2
- 150000004665 fatty acids Chemical class 0.000 description 2
- 238000009285 membrane fouling Methods 0.000 description 2
- 238000000034 method Methods 0.000 description 2
- 239000012466 permeate Substances 0.000 description 2
- 238000001223 reverse osmosis Methods 0.000 description 2
- 239000010865 sewage Substances 0.000 description 2
- 239000010802 sludge Substances 0.000 description 2
- 125000006850 spacer group Chemical group 0.000 description 2
- WQZGKKKJIJFFOK-GASJEMHNSA-N Glucose Natural products OC[C@H]1OC(O)[C@H](O)[C@@H](O)[C@@H]1O WQZGKKKJIJFFOK-GASJEMHNSA-N 0.000 description 1
- -1 N2 gas Chemical compound 0.000 description 1
- 240000004808 Saccharomyces cerevisiae Species 0.000 description 1
- 230000001476 alcoholic effect Effects 0.000 description 1
- 239000000969 carrier Substances 0.000 description 1
- 238000005266 casting Methods 0.000 description 1
- 238000012258 culturing Methods 0.000 description 1
- 239000008103 glucose Substances 0.000 description 1
- 238000001471 micro-filtration Methods 0.000 description 1
- 230000000813 microbial effect Effects 0.000 description 1
- 239000004745 nonwoven fabric Substances 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 239000008213 purified water Substances 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 239000011347 resin Substances 0.000 description 1
- 229920005989 resin Polymers 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 241001148471 unidentified anaerobic bacterium Species 0.000 description 1
- 238000004078 waterproofing Methods 0.000 description 1
- 239000002023 wood Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
- C12M29/00—Means for introduction, extraction or recirculation of materials, e.g. pumps
- C12M29/04—Filters; Permeable or porous membranes or plates, e.g. dialysis
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
- C12M29/00—Means for introduction, extraction or recirculation of materials, e.g. pumps
- C12M29/06—Nozzles; Sprayers; Spargers; Diffusers
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
- C12M39/00—Means for cleaning the apparatus or avoiding unwanted deposits of microorganisms
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
- C12M41/00—Means for regulation, monitoring, measurement or control, e.g. flow regulation
- C12M41/30—Means for regulation, monitoring, measurement or control, e.g. flow regulation of concentration
- C12M41/34—Means for regulation, monitoring, measurement or control, e.g. flow regulation of concentration of gas
Landscapes
- Chemical & Material Sciences (AREA)
- Wood Science & Technology (AREA)
- Life Sciences & Earth Sciences (AREA)
- Engineering & Computer Science (AREA)
- Bioinformatics & Cheminformatics (AREA)
- Health & Medical Sciences (AREA)
- Organic Chemistry (AREA)
- Zoology (AREA)
- Biomedical Technology (AREA)
- Sustainable Development (AREA)
- Microbiology (AREA)
- Biochemistry (AREA)
- General Engineering & Computer Science (AREA)
- General Health & Medical Sciences (AREA)
- Genetics & Genomics (AREA)
- Biotechnology (AREA)
- Analytical Chemistry (AREA)
- Apparatus Associated With Microorganisms And Enzymes (AREA)
Abstract
Description
【発明の詳細な説明】
〈産業上の利用分野〉
本発明は嫌気性微生物による発酵を効率よく行い得る膜
処理装置に関するものである。DETAILED DESCRIPTION OF THE INVENTION <Industrial Application Field> The present invention relates to a membrane treatment device that can efficiently carry out fermentation using anaerobic microorganisms.
〈先行技術と問題点〉
嫌気性微生物を用いる発酵プロセスは、有機物質を含む
原液からメタンガスを回収する最終グロセスとしてのメ
タン発酵を初め、嫌気条件でのアルコール発酵など有用
な微生物利用法として注目されている。<Prior art and problems> Fermentation processes using anaerobic microorganisms have attracted attention as useful microbial utilization methods, including methane fermentation as a final process for recovering methane gas from raw solutions containing organic substances, and alcohol fermentation under anaerobic conditions. ing.
しかしながら、従来においては嫌気発酵を回分式によっ
て行っており、微生物の生育速度が遅いために、反応に
長期間を要し、大規模な発酵槽設備が不可欠である。However, conventionally, anaerobic fermentation has been carried out in a batch manner, and due to the slow growth rate of microorganisms, the reaction requires a long period of time, and large-scale fermentor equipment is indispensable.
最近においては、高分子に包括または無機担体に吸着さ
せた微生物を用いて、嫌気発酵を連続的に高速下で行う
ことが試みられているが、微生物の固定が困難であって
当該微生物の処理液中への混合が不可避的に発生し、そ
の分離操作が必要となり、やっかいである。Recently, attempts have been made to perform anaerobic fermentation continuously at high speed using microorganisms entrapped in polymers or adsorbed on inorganic carriers, but it is difficult to immobilize the microorganisms and the processing of the microorganisms is difficult. Mixing into the liquid inevitably occurs, and a separation operation is required, which is troublesome.
〈発明の目的〉
本発明の目的は、精密ｐ過膜、限外濾過膜や逆浸透膜を
用いて、嫌気性微生物の高濃度での連続培養を可能なら
しめることにより、反応時間の短縮化、発酵槽の小型化
を図ることにある。<Objective of the Invention> The object of the present invention is to shorten reaction time by enabling continuous cultivation of anaerobic microorganisms at high concentrations using precision p-filtration membranes, ultrafiltration membranes, and reverse osmosis membranes. The aim is to downsize the fermenter.
〈発明の構成〉
本発明に係る膜処理装置は、嫌気性微生物を含む発酵槽
内に膜装置と、噴出非酸素性ガスにより膜面に気液混合
流を接触させるためのガス噴出手段とを設け、膜装置に
対し膜面に差圧を作用させるための差圧手段を設けたこ
とを特徴とする構成である。<Configuration of the Invention> The membrane treatment device according to the present invention includes a membrane device in a fermenter containing anaerobic microorganisms, and a gas jetting means for bringing a gas-liquid mixed flow into contact with the membrane surface using jetted non-oxygen gas. This configuration is characterized in that a differential pressure means is provided for applying a differential pressure to the membrane surface of the membrane device.
上記において、発酵槽内の菌体濃度を高濃度にしても、
膜面上での濃度分極、膜汚損を膜面上での気液混合流の
ために効果的に防止できる。In the above, even if the bacterial cell concentration in the fermenter is made high,
Concentration polarization on the membrane surface and membrane fouling can be effectively prevented due to the gas-liquid mixed flow on the membrane surface.
従って、膜の透過作用を効率よく行なわせることができ
、これにより菌体濃度を高濃度にでき、この菌体の高濃
度下、発酵を高速度にて行なわせることができる。Therefore, the permeation effect of the membrane can be carried out efficiently, and thereby the bacterial cell concentration can be increased, and fermentation can be carried out at a high speed under the high bacterial cell concentration.
かかる反応の高速度下では、嫌気性菌によるガスの産出
量が犬であり、このガスを上記気液混合流を得るための
ガス源として利用できる。Under such high rates of reaction, the anaerobic bacteria produce a large amount of gas, which can be used as a gas source to obtain the gas-liquid mixed stream.
〈実施例の説明〉 以下、図面により本発明を説明する。<Explanation of Examples> The present invention will be explained below with reference to the drawings.
第２図において、１は密閉型発酵槽であり、ガス噴出手
段例えば、散気管２（多孔パイプ）を設けである。この
散気管２に送気管２１により非酸素性気体例えばＮ２ガ
スを圧送し、散気管から気泡を散出させ、その散気流（
気・液混合液）Ｋよって処理液を循環させると共に液中
の嫌気性微生物により発酵を行う。In FIG. 2, reference numeral 1 denotes a closed fermentation tank, which is equipped with gas ejection means, for example, an aeration pipe 2 (porous pipe). A non-oxygen gas, such as N2 gas, is force-fed through the air diffuser pipe 21 through the air diffuser pipe 21, air bubbles are dispersed from the air diffuser pipe, and the air diffuser flow (
The treatment liquid is circulated by the gas/liquid mixture) and fermentation is carried out by the anaerobic microorganisms in the liquid.
３は膜装置であり、上記散気管２の直上に配設しである
。この膜装置は、散気管２からの気・液混合流を通過さ
せる鉛直方向通路３１．３１・・・ を有しており、こ
の通路において気・液混合流が膜面に接触し、膜面上で
の有機物質の濃度分極、膜面の嫌気性微生物による汚損
を防止できる。４は膜装置３の透過水側を減圧し、移送
するための真空引きポンプであり、これにより透過水を
膜装置３から取出すことができる。Reference numeral 3 denotes a membrane device, which is disposed directly above the aeration pipe 2. This membrane device has vertical passages 31, 31... through which the gas/liquid mixed flow from the aeration tube 2 passes, and in these passages, the gas/liquid mixed flow contacts the membrane surface, and the membrane surface Concentration polarization of organic substances on the membrane surface and contamination of the membrane surface by anaerobic microorganisms can be prevented. Reference numeral 4 denotes a vacuum pump for reducing the pressure on the permeated water side of the membrane device 3 and transferring it, so that the permeated water can be taken out from the membrane device 3.
膜装置３の透過水側を減圧する代りに、発酵槽を大気圧
以上に加圧して膜間差圧を得ることもできる。これらの
減圧・加圧を併用することもできる。６はポンプであり
、連続的に被処理液を供給して、連続反応を行う場合に
使用する。Instead of reducing the pressure on the permeated water side of the membrane device 3, it is also possible to pressurize the fermenter above atmospheric pressure to obtain a transmembrane pressure difference. These depressurization and pressurization can also be used together. Reference numeral 6 denotes a pump, which is used to continuously supply the liquid to be treated and perform continuous reactions.
上記において、得られる透過水は被処理液により異なる
が、通常の発酵プロセスにおいては有用な低分子有機物
質の溶液であり、汚水処理においては、浄水である。In the above, the obtained permeated water differs depending on the liquid to be treated, but in normal fermentation processes it is a solution of useful low-molecular organic substances, and in sewage treatment it is purified water.
上記発酵に伴い発生する非酸素性ガスは排ガス管により
一部を抜き皐りつつ、または抜き取ることなく全部をポ
ンプ７により散気装置に循環させ得る。この非酸素性ガ
ス、すなわち、嫌気性微生物の産生気体が発酵促進に及
ぼす度合に応じ、上記抜き取り量を調整すればよい。The non-oxygen gas generated during the fermentation can be partly extracted through the exhaust gas pipe, or the whole can be circulated to the air diffuser by the pump 7 without being extracted. The amount to be extracted may be adjusted depending on the degree to which this non-oxygen gas, that is, the gas produced by anaerobic microorganisms, affects fermentation promotion.
産生ガスがメタンの場合、他のガス（Ｎ２ガス）と分離
しエネルギー源として回収することが有効である。When the produced gas is methane, it is effective to separate it from other gases (N2 gas) and recover it as an energy source.
上記膜分離装置３には、ノズル２からの噴出ガスにより
濃度分極・膜汚損等を防止できるものであれば、適宜の
ものを使用できる。例えば、内径約１ＯＮ以上の管状膜
を複数本並べた、いわゆるパラレル型流路の膜モジュー
ル、あるいは任意の巾の平膜型（例えば、スパイラル型
、プリーツ型）あるいは平板型の膜エレメントを上記鉛
直通路を確保するように組立てた膜モジュールを使用で
きる。かかる膜モジュールの鉛直方向の長さは発酵槽の
深さによって異るが、通常は発酵槽の深さから０．３ｍ
を減じた長さであり、一般に０．５ｍ以上である。これ
らは敷部に分割した型式で使用することもできる。Any suitable membrane separator 3 can be used as long as it can prevent concentration polarization, membrane fouling, etc. caused by the gas ejected from the nozzle 2. For example, a membrane module with a so-called parallel flow path in which a plurality of tubular membranes with an inner diameter of about 1ON or more are lined up, or a flat membrane type (for example, spiral type, pleated type) or flat plate type membrane element of any width can be connected to the above-mentioned vertical line. Membrane modules assembled to ensure passage can be used. The vertical length of such a membrane module varies depending on the depth of the fermenter, but is usually 0.3 m from the depth of the fermenter.
It is generally 0.5 m or more. These can also be used in a divided form.
上記スパイラル型等の平膜型の膜エレメントにおいては
、上記した鉛直通路中に流路スペーサを設けないことが
望ましい。何れの膜エレメントにおいても、鉛直通路の
厚みは１０寵以上とすることが望ましい。しかし、その
厚みを余り大きくすると、設置できる膜面積が減少する
ので好ましくない。In a flat membrane type membrane element such as the spiral type described above, it is desirable that no flow path spacer is provided in the above-mentioned vertical passage. In any membrane element, it is desirable that the thickness of the vertical passage be 10 cm or more. However, if the thickness is too large, the area of the membrane that can be installed will be reduced, which is not preferable.
第２図Ａは本発明において使用する膜装置の一例を示し
、不織布等の多孔支持管３２上に膜３３を設けた管状膜
３０を数本、外筒３４内に納め（第２図Ｂ参照）、両端
をエンドプレート３５．３５または注型樹脂によって封
止した構成であり上記の気・液混合流は管状膜内を流動
し、透過水は外筒内より透過木取出口を経て取出される
。膜には、精密濾過膜、半透膜、特に限外濾過膜あるい
は食塩除去率の低い、いわゆるル−ズ逆浸透膜を用いる
。FIG. 2A shows an example of a membrane device used in the present invention, in which several tubular membranes 30, each having a membrane 33 provided on a porous support tube 32 made of non-woven fabric, are housed in an outer cylinder 34 (see FIG. 2B). ), both ends are sealed with end plates 35, 35 or casting resin, the above-mentioned gas/liquid mixed flow flows within the tubular membrane, and permeated water is taken out from the outer cylinder through the permeable wood outlet. Ru. The membrane used is a microfiltration membrane, a semipermeable membrane, especially an ultrafiltration membrane, or a so-called loose reverse osmosis membrane with a low salt removal rate.
第３図Ａは本発明において使用する膜装置の別例を示し
、一対の透過水集水管３５．３５に第３図Ｂにも示すよ
うに平板型膜（平膜３３．３３間に透過水路用スペーサ
３６を介在させたもの）を連通し、これをユニットとし
てホルダーにより一定の間隔で並設しである。この膜エ
レメントの場合、ユニット間に散気管を配設することが
できる。FIG. 3A shows another example of the membrane device used in the present invention, in which a pair of permeate water collecting pipes 35, 35 are connected to a flat plate type membrane (a permeate channel between the flat membranes 33, 33) as shown in FIG. 3B. (with a spacer 36 interposed) are communicated, and the units are arranged side by side at regular intervals by a holder. In the case of this membrane element, diffuser pipes can be arranged between the units.
本発明に係る膜処理装置においては、上記した通り発酵
槽内の菌体濃度を高濃度になし得、その濃度は通常、２
０〜２００ ｆｙ＃である。この結果、被処理液の反応
滞留時間を４〜６時間といった短時間になし得、発酵槽
の容量を従来の１／３〜１／１０に縮小できる。ががる
発酵槽の小型化のもとでは、濃度分極防水のための気液
混合流を得るのに必要なガス量（１〜１．５ ｒｎ／
ｓ ）を相当に小量化でき、時間肖り発酵槽容量の約２
倍量のガスを供給すれば充分である。In the membrane treatment apparatus according to the present invention, as described above, the bacterial cell concentration in the fermenter can be made high, and the concentration is usually 2.
0 to 200 fy#. As a result, the reaction residence time of the liquid to be treated can be shortened to 4 to 6 hours, and the capacity of the fermenter can be reduced to 1/3 to 1/10 of the conventional capacity. With the miniaturization of the Gagaru fermenter, the amount of gas required to obtain a gas-liquid mixed flow for concentration polarization waterproofing (1~1.5 rn/
s) can be considerably reduced, and approximately 2 times the fermenter capacity
It is sufficient to supply double the amount of gas.
実施例１
有効容積５０１の発酵槽内に、内径１２ｍｍ０１長さ４
０ ｃｒｎ、管状限外ａ・！過膜３０本（膜面積０．４
５ｍ１ ）からなる膜装置を設置し、下水処理場から採
取した消化汚泥を加えて、３０００ｐｐｍの低級脂肪酸
を含む処理液をｌＱｌ／ｈｒ で通液した。Example 1 In a fermenter with effective volume 501, inner diameter 12 mm01 length 4
0 crn, tubular limit a・! 30 membranes (membrane area 0.4
A membrane device consisting of 5 m1) was installed, digested sludge collected from a sewage treatment plant was added, and a treatment solution containing 3000 ppm of lower fatty acids was passed through at a rate of 1 Ql/hr.
膜装置の下部に設けた散気装置から非酸素性ガスを１０
０１／ｈｒで吹き込み、０．５ ｋｇ／ｄの加圧下で排
出されるガスの５０％を再び発酵構内に戻して培養を行
ったところ、３日後には約１０１／ｈｒ で得られる
膜透過水の低級脂肪酸濃度は５０ＰＰｍ以下となり、ｌ
７ ｌ／ｈｒで生成されるメタンガスが得られた。こ
のときの汚泥の濃度は２２ｙ／ｌであった。10% of non-oxygen gas is supplied from the air diffuser installed at the bottom of the membrane device.
When 50% of the gas discharged under a pressure of 0.5 kg/d was returned to the fermentation premises and cultured, after 3 days, membrane permeated water obtained at a rate of about 101/hr was obtained. The lower fatty acid concentration of is less than 50PPm, and l
Methane gas produced at 7 l/hr was obtained. The concentration of sludge at this time was 22 y/l.
実施例２
上記の発酵槽内に、１０αＸ ４０ｃｒｎの平膜型限外
（′濃過モジュール（平膜２６枚、膜面積約１ｍ′）を
設置し、酵母培養によるアルコール発酵を行った。２０
％グルコース溶液の滞留時間を４時間とし、発生するＣ
Ｏ２ガスの５０％を散気装置から循環させ、連続培養を
行ったところ、２週間にわたって７〜８％のアルコール
溶液が得られた。Example 2 A 10αX 40 crn flat membrane type ultra-filtration module (26 flat membranes, membrane area approximately 1 m) was installed in the above fermenter, and alcoholic fermentation by yeast culture was carried out.20
% glucose solution residence time was 4 hours, and the generated C
When 50% of O2 gas was circulated through the air diffuser and continuous culture was performed, a 7-8% alcohol solution was obtained over two weeks.
〈発明の効果〉
本発明に係る膜処理装置は上述した通りの構成であり、
発酵槽内の菌体濃度を高くしても発酵を円滑に行なわせ
ることができ、嫌気性微生物の高濃度培養による発酵時
間の短縮（或いは処理景の増大、生成物量の増加）、設
備の簡易化（装置の小型化、運転動力の低減）を図るこ
とができる。<Effects of the Invention> The membrane treatment apparatus according to the present invention has the configuration as described above,
Fermentation can be carried out smoothly even if the bacterial cell concentration in the fermenter is increased, and by culturing anaerobic microorganisms at a high concentration, the fermentation time can be shortened (or the processing environment can be increased, or the amount of product can be increased), and the equipment can be simplified. (miniaturization of the device, reduction of operating power).
第２図は本発明に係る膜処理装置を示す説明図、第２図
Ａは本発明において使用する膜装置を示す説明図、第２
図Ｂは第２図Ａにおけるｂ−ｂ断面説明図、第３図Ａは
本発明において使用する膜装置の別例を示す説明図、第
３図Ｂは第３図Ａにおけるｂ−ｂ断面説明図である。
図において、１は発酵槽、２は散気装置、３は膜装置、
７は送気ポンプである。
？FIG. 2 is an explanatory diagram showing a membrane treatment apparatus according to the present invention, FIG. 2A is an explanatory diagram showing a membrane apparatus used in the present invention, and FIG.
Figure B is an explanatory diagram of the bb cross section in Figure 2 A, Figure 3 A is an explanatory diagram showing another example of the membrane device used in the present invention, and Figure 3 B is an explanatory diagram of the bb cross section in Figure 3 A. It is a diagram. In the figure, 1 is a fermenter, 2 is an aeration device, 3 is a membrane device,
7 is an air pump. ?
Claims (2)
酸素性ガスにより膜面に気液混合流を接触させるための
ガス噴出手段を設け、膜装置に対し膜面に差圧を作用さ
せるための差圧手段を設けたことを特徴とする膜処理装
置。(1) A membrane device is provided in a fermenter containing anaerobic microorganisms, and a gas jetting means for bringing a gas-liquid mixed flow into contact with the membrane surface using jetted non-oxygen gas is provided, and a differential pressure is applied to the membrane surface with respect to the membrane device. A membrane processing device characterized by being provided with differential pressure means for applying pressure.
全部を非酸性ガスとして使用し得る手段を、ガス噴出手
段に具備させたことを特徴とする特許請求の範囲第２項
記載の膜処理装置。(2) The membrane treatment according to claim 2, characterized in that the gas ejection means is equipped with a means for using part or all of the gas produced by the anaerobic microorganisms as a non-acidic gas. Device.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP8981886A JPS62244378A (en) | 1986-04-17 | 1986-04-17 | Device for pretreatment of filtration membrane |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP8981886A JPS62244378A (en) | 1986-04-17 | 1986-04-17 | Device for pretreatment of filtration membrane |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPS62244378A true JPS62244378A (en) | 1987-10-24 |
Family
ID=13981328
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP8981886A Pending JPS62244378A (en) | 1986-04-17 | 1986-04-17 | Device for pretreatment of filtration membrane |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS62244378A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP2714885A4 (en) * | 2011-04-26 | 2015-05-27 | Therapeutic Proteins Internat Llc | Concentrator filter |
| CN108866133A (en) * | 2018-07-12 | 2018-11-23 | 天津科技大学 | Pressure difference pretreatment collaboration high density fermentation wheat bran produces wheat bran oligopeptide method |
-
1986
- 1986-04-17 JP JP8981886A patent/JPS62244378A/en active Pending
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP2714885A4 (en) * | 2011-04-26 | 2015-05-27 | Therapeutic Proteins Internat Llc | Concentrator filter |
| US9364776B2 (en) | 2011-04-26 | 2016-06-14 | Sarfaraz K. Niazi | Concentrator filter |
| CN108866133A (en) * | 2018-07-12 | 2018-11-23 | 天津科技大学 | Pressure difference pretreatment collaboration high density fermentation wheat bran produces wheat bran oligopeptide method |
| CN108866133B (en) * | 2018-07-12 | 2022-03-04 | 天津科技大学 | Method for producing wheat bran oligopeptide by virtue of synergistic high-density fermentation of wheat bran through differential pressure pretreatment |
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